Process of converting oils



, o. P. AMEND PBOCESS OF CONVERTING OILS Filed June 8, 1917.

2 Sheets-Sheet 1 Gal-21, 1924. v 1,512,264

. o. P. AMEND v PROCESS OF CONVERTING 0111s Fil ed June a, 1917[Sheets-Sheet 2 3 wue'nto 0 FQJZALmeWJ;

' naphthas and gasolines,

- shale,

. tion engines,

rates OTTO P. AMEND, OF NEW YORK, N. Y.

PROCESS OF CONVERTING OILS.

Application filed June 8 To all whom it may concern:

Be it known that I, O'rro P. AMEND, a

citizen of the United States of America, residing in the borough ofManhattan, city, county, and State of New York, have in-. vented certainnew and useful Processes of Converting Oils. This invention relatesbroadly to the art of cracking crude petroleum, .kerosene, or otherhigher boiling hydrocarbon distillates, orresi'duals,that is,hydrocarbons having boiling points above 130 (1, and converting the sameinto lower boiling and even petrolic ethers, suitable for use ininternal combusand for all other purposes-for which low boilinghydrocarbon distillates are used.

The process is applicable either to the treatment ofcrude petroleum orto any of the higher boiling petroleum distillates, such as, heavynaphthas, kerosenes, gas oils, fuel oils, or even heavier hydrocarbonproducts or to any kerosene or burningoil, or higher boilinghydrocarbons derived from bituminous coal, source derived. Where crudepetroleum is treated by my process, the low boilinghy- .drocarbonswithin the gasoline limits should preferably be first removed, usuallyby or clinarvmthods of fractional distillation.

a suitable cracking Hitherto, processes hydrocarbons, siduals, toproduce therefrom low boiling hydrocarbon distillates, where thecracking takes place -in largestills, have. generally been carried outby the use of heat externally applied to the still. In order to obtaintemperature in the intemuch higher tem-.

for cracking heavy rior of theoil itself, very peratures must beexternally'applied to the I metal sides and bottom of the sun, or tointerior tubes,- with'thersult that the metal sides and bottom, or theinterior tubes, are

extremely hot, and result in extensive overcracking of those portions ofthe oil coming in direct contact with the heated metal, producing anundesirable unsaturated'cracked product. A further disadvantage ofexternal heating lies in the fact that, if the iron, ofwhich the stillsare generally made, is heated to the high external heat necessarytoproduce a cracking temperature within the oil itself, and the resultof thecracking of the -oils being also to cause a'heavy depositionnofcarbon upon the sides and or from whatever crude oils, distillates, orre- 1917. Serial No. 173,667.

bottom of the still,this deposition of carbon in the case of a large onethousand barrel still amounting to as much as from 350 pounds to over1000 pounds of deposited carbon,the red hot iron of'the still sides andbottom is chemically affected by the depositing carbon, with theresulting production of carbide of iron and the rapid deterioration ofthe metal in its ability to withstand pressure, as well as the rapiddestruction of the bottom of the still. Because of this result, it hasbeen found .necessary to have as many as five false still bottoms in asingle still, by which'the carbon resulting from the cracking operation,is klept away from the structural iron of the sti Up to the presenttime, kerosene, that is to say, a mixture of hydrocarbons having aboiling point range not in excess of between 130 C. and 260 myknowledge, been successfully cracked in large stills and converted intoa low 'boiling distillate. I have discovered a method by which kerosene,as well as higher boil-' ing hydrocarbons and crude oil, may be crackedand converted into a low boiling hydrocarbon distillate in large stillsby subjecting the liquid hydrocarbons in the still to a. suitabledissociating temperature for 0., has never, to

tocontact with carbon heated electrically the particular hydrocarbon ofbetween-a red and a white heat, while maintaining" the liquid and vaporhydrocarbons both' in the still and condenser under any desired"autogenous pressure in. excess {of atmospheric up to two inch, orhigher, tainin-g relatively cool the-- the still or container.

I The essential difierence ess and. previous. processes uid hydrocarbonsin large stills or'refceptacles and .at the same time IIlfilIF metalparts of between my procby heat and pressure,;confs1sts in'the fact thatin previous processes of the high boiling hydrocarbon is producedchiefly by the'back action of pressure of the --'e"volved hydrocarbonvapors, the amount of heat applied to the liquid hydrocarbon being forcracking liqthe dissociation hundred-pounds to the square I generallyonly sufiicient to produce the necessary evolution of vapors'andconsequent autog'enous pressure. In' previous pressure processes, it isthe action of the pressure upon the heated hydrocarbons, rather thananydirect dissociating action of the heat itself, that is relied on tocrack the heavy .hydrocarbons. By my process, however, the

cracking or dissociation of kerosene or other higher boiling liquidhydrocarbons 1s produced directly and initially by enforclng contact orclose proximity With highly heated carbon, this carbon, being preferablyheated by the passage of an electric current, or by induction. In myprocess, the action of the pressure of the evolved vapors,' which; neednot be more than in excess of atmospheric and below four atmospheres, isnot, as in previous processes, to produce the dissociation of thehydrocarbons, but merely to force the liquid hydrocarbons and theirevolved vapors back upon, the incandescent or highly heated carbon. Inprevious processes, initial vaporization of the hydrocarbons is reliedon to produce the pressure, which, upon reaching a certaln point,effects the cracking, or dissociation of the hydrocarbons. In myprocess, the initial dissociation of the high boiling hydrocarbons isinstantaneous upon the contact of the hydrocarbons with the highlyheated carbon, and the pressure produced by the evolved vapors is usedmerely to facilitate this intimate contact between the hydrocar- I bonand the heated carbon.

One of the chief difliculties hitherto experienced in attempts atcracking and converting high boiling hydrocarbons into a low boilingdistillate, by the use of a me' tallic resistor submerged Within the oiland heated to incandescence, consists in the fact that when the metalresistor Was heated to the high heat required for successful cracking ofthe kerosene or other high boiling hydrocarbon, in the case of kerosene,a temperature corresponding to that of from a cherry red to a bright redor a White heat being generally required, the heated resistor -repelledthe oil and prevented intimate contact, and the oil at a distance fromthe resistor was merely vaporized without being cracked or convertedinto lighter hydrocarbons. The greater part of the condensate obtainedwas, therefore, unconverted oil. Any pressure in excess of atmosphericthat is sufiicient or suitable to keep the liquid hydrocarbon, or theevolved hydrocarbon vapors, or both, in contact with or close proximityto the electrically heated carbon, or other high resistance conductor,or other source of heat, so as to produce thereby dissociation of thehigh boiling hydrocarbon into low boiling vapors, is suflicient. Wherethe carbon or other high resistance conductor is heated toa temperaturecorresponding 7 a White'heat, and more particularly, where it is heatedto l a bright red, or between a bri'ghtred and sirable.

a white heat, pressures ranging from about 20 to 150 pounds to thesquare inch are de- Generally, higher pressures are preferable to lowerpressures, for the reason first be removed by injecting an ten pounds tothe square inch up to four atmospheres, the cracked hydrocarbon condensate being released at the regulated pressure by the action of acheck valve. I have also produced a low boiling distillate from keroseneunder substantially the same heat conditions at pressures ranging fromfour atmospheres up to 200 pounds to the square inch. It is, therefore,obvious that pressures of four atmospheres or over are unnecessary evento convert kerosene into a low boiling distillate, the only effectof theincreased pressure being to produce more intimate contact between thehydrocarbon and the heating element.

By my process, I am able to secure any desired cracking or dissociatingtemperature within the interior of the oil itself, at the same time thatthe sides and bottom of the still or container are relatively cool, andthe ability of the metal of the still to resist high pressures is notseriously impaired. I secure this result by internal electrical heatingof the oil and its evolved vapors by means of one or more highresistance resistors, preferably made of carbon, heated to- Whatevercracking or dissociating temperature is desired.

This electric heating either entirely immersed in the oil, or it may beentirely above the surface of the liquid, or one or more of suchelectric heating elements may be either Wholly submerged or partiallyimmersed in the oil, and at the same time, one or more of such. electricheating elements may be inserted in a suitable space above the liquid tosecure an intimate contact with the evolved hydrocarbon vapors. Wherethe electric heating element is Wholly or partly above the surface ofthe liquid, all air should inert gas free from oxygen, such as hydrogengas or natural gas, or if one or more resistors are entirely submergedin the oil, and one or more are above the surface of the oil, thecurrent onto. the submerged resistor until the hydrocarbon vaporsevolved, which, are allowedto. escape, have ,driven -ofi' all airelement may 1 be may be first turned ltHl above the surface of the oil,in the-container and only then is the current turned on to the resistorsor other electric heating elements above the oil. Where an electricheatlng element is located entirely above the surfacelof the oil, Iprefer to fill th space above the oil with hydrogen gas, before turningon the current. There is a very distinct advantage in having one or moreelectric heat-' ing elements located above the surface of the oil in thestill or container, or partially submerged and partially above thesurface of the liquid, as by this means more intimate contact is hadbet-ween the heating element and the evolved hydrocarbon vapors, andsuch liquid hydrocarbons as have only been vaporized without cracking orconversion into lighter vapors, because of the conduction of heat fromthe heating element in the heated carbon tubes, either filled with aporous mass of carbon, such as broken charcoal, or petroleum coke,shouldsubstantially fill a cross section of the vapor dome or the pipe oroutlet leading I to the condenser, such as shown in my copendinapplication Serial No. 173,668, filed une 8, 1917. In this way, all ofthe evolved hydrocarbon vapors must pass in contact with the heatedcarbon. Where an electric heating element located above the surface ofthe liquid as above de scribed, is used, much lower pressures may besuccessfully used than where the sole source of heat is located withinthe liquid hydrocarbon. In addition, the hydrocarbons in the vapor stageare much more expeditiously cracked than liquid hydrocarbons.

By the use of internal heat, electrically .applied, I am able toregulate to a nicety the actual cracking temperature within the body ofth oil or its evolved vapors, which is practically impossible whereexternal heating is resorted to. This more perfect regulation of theheat within the oil enables a more constant quality of cracked productto be produced than is possible with external heating of the still, andalso a product much freer from terpenes and other highly unsaturatedundesirable 'oxidizable hydrocarbons.

With the use of carbon resistors, there is substantially-no depositionof carbon, and the condensate or distillate is composed substantially ofsaturated hydrocarbons. .Contrary to all preconceived ideas, the higherthe heats used with carbon resistors even up to a white heat, the freeris the condensate from unsaturated hydrocarbons and the freer it is fromcoloring matter.

The upper part of the still or cracking retort in which the liquidhydrocarbons are to be cracked by being brought in contact with theheatedcarbon resistors, should preferably be equipped witha vapor domeor tower of suitable height in comparison to I the size of the still orretort, so that the greater part of the heavy unconverted hydrocarbonvapors will condense and fall back into the heated zones for recracking.

From the upper part of this vapor dome or tower, an inclined conduit orrunback preferably leads up to the condenser coil. This inclinedconduit, while not necessary,

is distinctly advantageous, as it obviates the necessity of making thevertical vapor dome or to-wer'too high, and roduces the effect ofincreasing the length -0. the reflux condensation zone. The operationof-the air cooled inclined conduit is to condense the heavier fractionsof the distillate and automatically to return them to the heated zonesof the still for further treatment. This inclined ,conduit may be of anydesired length and diameter depending on the size of the still and theamount of vapors requiring to pass. over in a given time. The heavierhydrocarbon vapors are subjected to condensation under pressures in therunback and returned to the still and subjected again to the disso-'ciating action of the heated carbon, the light vapors passing over tothe condenser.

I have found that by subjecting the liquid and vaporized hydrocarbon topressures of the evolved vapors in excess of atmospheric and preferablyin excess of ten pounds to the square inch and up to as high as fivehundred pounds to the square inch, and by imparting a suitabletemperature to dissociate the hydrocarbons, while such hydrocarbons arein direct contact with the electrically heated* carbon resistors, Iobtain a condensate containing a' higher percentage of low boilinghydrocarbons than where no pressure is used. Any desired regulatedpressure up to five hundred pounds to the square inch, may be obtainedby the use of a suitable check valve, which valve is set to open at thedesired pressure. In practice, the pressures used are below two hundredpounds to the square inch. This check valve'is placed beyond thecondenser, that is, between the pondenserv and the reservoir for thecondensate,'so that the condensation of the vapors, as well as it, intoa receiving tank or reservoir; I have found that the'eflectof'carbonwhen heated to a temperature corresponding to that from a red to a whiteheat, pref erably by electrical means, is to crack kerosene and otherhigher boiling hydrocarbons and convert them into low boilinghydrocarbons, with a practical absence of gas losses or of carbondeposition, even when comparatively high cracking temperatures are used,to a minimum of gas losses and a minimum of deposition of carbon, wheneven such high temperatures are used as would normally, by any processof external heating, decompose the hydrocarbon into fixed gases andcarbon. In other words, the effect of the cracking of the hydrocarbonvapors by the use of carbon heated to a temperature corresponding tothat ranging, from a red to a white heat, either by the passage of anelectric current is apparently protective to the hydrocarbons, in thatit prevents the formation of the end products,-fixed gases, hydrogen andcarbon, in any quantity, and keeps the dissociated hydrocarbon withinthe limits of a vapor that is capable of condensation into a low boilinghydrocarbon distillate, with a minimum of gas loss. l have further foundthat the higher the carbon is heated, even to a temperaturecorresponding to that of a white heat, the smaller is the percentage ofunsaturated hydrocarbons in the resulting distillate. By saturatedhydrocarbons, I mean hydrocarbons of the paraflin or of the naphtheneseries, or hydrocarbons of the benzene series, such as benzol, toluol,Xylol, etc. These latter benzene hydrocarbons, are however, not presentin any quantity in my distillate, it being substantially composed--\either of naphthene hydrocarbons or of a mixture of parafiin andnaphthene hydrocarbons. The extremely objectionable terpene,hemiterpene, and asphaltic hydrocarbons, are conspicuous for theirabsence from my condensate when carbonis used heated to from a brightred to a white-heat. As a result, therefore, of the practical absence ofgas losses and of carbon deposition, and the further absence ofundesirable unsaturated hydrocarbons from the distillate, I am able .toobtain a very high recovery, close to ninety per cent, of low boiling.distillate from the high-boiling hydrocarbons treated.

The degree of heat to which the hydrocarbons should be subjected bycontact with the heated resistors or heated carbon, may

depend in any given case both upon the character of the hydrocarbon tobe treated and also upon the character of the distillate desired to beproduced. For instance, kerosene should besubjected to contact withcarbOI1 heated preferabl to from a bright red to a white heat. rackingtemperatures for kerosene. may be used ranging from those of a cherryred heat to a white heat, that is approximately from 700" G. to 2000 (l,or higher. l-prefer a temperature eases-e ranging from that of a brightred to a white heat. Where a gas oil or a fuel oil is to be cracked, thecarbon may be heated to be tween a visible red and a white heat andpreferably, as with kerosene, to a bright red heat. Generally, with gasoils or fuel oils, cracking temperatures of between 000 voltage andlowamperage may be used. I

have obtained good results with carbon re sistors using a current of 77volts and 18 amperes. Generally, a current of between and 120 volts andbetween 14 and 20 amperes, is satisfactory, or a current of 12 to 15volts and from 100 to 150 amperes.

lVhen tested with concentrated sulphuric acid, practically nounsaturated hydrocarbons were found to be present in the condensateproduced by the present process. I have also obtained highly volatilesaturated distillates of a gravity of about 46 B. The high volatility,low boiling points, and high gravity of these distillates, combined withthe absence of ethylene or other unsaturated hydrocarbons, is explainedby the presence of a high percentage of volatile low-boiling naphtheneor polymethylene hydrocarbons. These naphthene hydrocarbons have a Baumgravity about 35 B. lower than the corresponding parafin hydrocarbons ofthe same carbon content, although their respective boiling points areonly about 12 C. abovethat of the corresponding parafiin. F or instance,the highly Volatile saturated naphthene hydrocarbon, hexymethylene (C Hhas a specific gravity of .793.

or a Baum gravity of onlyabout 45.6" B,

and a boiling point of 81 G whereas the gravity of only about ,53 B.,and notwithw y 120 standing has a boiling point of only 49 (1, ascompared with pentane (G H which has a Baum gravity of about 88 B. and aboiling point of about 37 0. Similarly, the naphthene hydrocarbonheptamethylene (C H has a specific gravity of .825, a Baum gravity ofabout 38 513., and a boiling point of 117 (1, and the naphtheneoctamethylene O I-I has a specific gravity of .850, a Baum gravity ofonly about 30' B. and a boiling point of 14:7 O. A gasoline equal partsof thenaphthene hydrocarbons.

(C H (c H land (Cl-I would have a specific gravity of about .79, or aBaum gravity of only about 46 B. As I have obtained a saturated crackeddistillate by my process having a specific gravity of .79 and a range ofboiling points from 52 B. up to about 150 C., it is obvious that thiscracked distillate must be chiefly composed of the naphthenehydrocarbons just described.

A certain proportion of the naphthene hydrocarbon tetramethylene (C H aswell as of pentamethylene (C l-I is obtained through compressing andcondensing the vapors obtained, uncondensable by ordinary cooling atatmospheric pressures. 'This naphthene hydrocarbon tetramethylene has aspecific gravity of .7 04, a Baum gravity of 6913. and a boiling pointof 11 G., and any considerable percentage of this hydrocarbon lowersconsiderably the specific gravity of the mixture. In order to clearlyshow the remarkable difference in the Baum and specific gravities of amixture of naphthene hydrocarbons on the one side and of paraifinhydrocarbons on the other, I have prepared the following table. In eachcase, I have taken a theoretical gasoline mixture containing equalpercentages of each of the homologous naphthene or paraffin hydrocarbonsrespectively included therein. I

. Baum gravity- Specific gravity. (.asolline mixtturte:

at on con en Paratfin. 552: Paraflin. iii g2 0 o (la-C bothinclusive.-." 81. 7 45. 1 656 .794 05-0 3 both inclusive 78. 7 41. 4 667808 0 -0 both inclusive. 75 37. 4 681 823 CrCa both inclusive. 82. 6 47654 787 The apparently high specific gravity and low Baum gravity ofthese distillates does not therefore militate in any way against theiruse as a high grade gasoline in internal combustion engines. Whereparaffin hydrocarbons are cracked, the specific gravity of the resultingcracked distillate is consider ably lower and the Baum gravityconsiderably higher, owing to the presence of a percentage of lightparaffin hydrocarbons in the distillate.

'Where carbon and particularly graphitic carbon resistors are used,heated to from a bright red to a white heat, a saturated hydro carboncondensate is obtained in the .first or the pressure may easilyoxidizable hydrocarbons and tarry or resinous colloidal matter, "whichmust subsequently be removed by well known methods. Where carbonresistors and high temperatures are used, only rectification ordephlegmation of the crude condensate is necessary, to obtain adistillate of the desired boiling points suitable for use in internalcombustion engines.

Instead of using simply carbon electrodes heated by the passage of anelectric current, an electric arc'may be produced within the oil, or thevapors above the oil, by passing an electric current through two carbonresistors kept a slight distance apart, both the resistors and theirleading-in and leadingout conductors being separated from contact withthe metallic parts of the still by suitable insulating material, such assoapstone, asbestos, or mica. v

It is, of course, understood that the hydrocarbon vapors coming overfrom the still may be passed through suitable dephlegmatorsby which allhydrocarbons boiling over the desired point of cut may be removed,thereby making rectification unnecessary. Rectification is, however,distinctly advantageous, as the redistillation apparently'produces afurther cracking of the condensate. The process may be made continuousby injecting from time to time additional oil into the still orcontainer. The oil may be pumped in from time to time, under pressure,by a suitable pump, be released during the introductionof the oil.

-By high-boiling liquid hydrocarbons, I mean to include all liquidhydrocarbons having boiling points above 130 C,

By a kerosene or burning oil, mean to include all liquid hydrocarbons,

either crude or refined, boiling between naphthene hydrocarbondistillate, I mean a low-boiling distillate composed principally ofhydrocarbons of the naphthene o-r polymethylene (C E series. As much asthirty to forty per cent of parafiin hydrocarbons may, however, bepresent in the distillate. v

The temperatures, .amperages, voltages, wattages and pressures, givenherein, are intended to be illustrative and not limiting".

Referring to the drawings, Figure 1 shows, more or lessdiagrammatically, partly in section and partly in elevation, asubstantially complete apparatus for practicing the process. v I

Figure 2 shows substantially the same type of apparatus except that thepipe connecting the outlet of the still to the condenser is not inclinedas it is in. Figure 1..

Figure 3 is a fragmentary view of the still, showing a modined way ofelectrically heating the contents thereof.

Referring particularly to Figure 1, A is a still having an oil inlet aand an inlet for inert gas 6 extending to nearly the bottom of thestill. The still is heated by means 4 of a submerged carbon resistor 0,preferably in tubular form as shown, the said resistor being providedwith suitable terminals (2 and e properly insulated from the walls ofthe still. The upper portion of the still may also be provided with acarbonresistor f for subjecting the oil vapors to heat, said resistorbeing preferably in tubular form, and being provided with suitableterminals 9' and h, also properly insulated from the walls of the still.The outlet or gooseneck B of the still is inclined as shown, whereby amore or less reflux effect is obtained. The gooseneck of the stillconnects with a coolmg coil or condenser D, positioned within a coolingjacket or casing E, said jacket being provided with a suitable inlet a"and outlet j for the cooling agent such as water. The outlet in from thecondenser is provided with a pressure valve C and leads to a suitabletrap or condensed liquid collector F having a baffle Z and a suitabledraw-off pipe m. The trap is provided with anoutlet it for non-condensedgases or vapors, said outlet leading to a suitable compressor G,diagrammatically shown, wherein said vapors or gases are compressed,whence they pass through, the outlet- 0 of the compressor into anexpansion chamber H. The effect of expanding the mixture of compressedgases and vapors in chamber H results in the reduction of thetemperature thereof to such extent that practically all the condensablevapors are liquefied in said chamber and may be drawn off through pipe7. The expansion chamber H is provided with a gas or vapor outlet 9through which the residuary, uncondensed vapors or gases pass, whereuponthey may be. subjected to such further use or treatment as is founddesirable.

Referring now to Figure 2, A. is a still having an oil inlet a and aninlet for inert gas 1) extending to nearly the bottom of the still. Thestill is heated by means of a submerged .carbon resistor 0, preferablyin tubular form as shown, the said resistor being provided with suitableterminals 03' and e properly insulated from the Walls of aeiaaee thestill. The upper portion of the still may also'be provided with a carbonresistor f for subjecting the oil vapors to heat, said resistor beingpreferably in tubular form,

The gooseneck of the still connects with a cooling coil or condenser D,positioned within a cooling jacket or casing E, said jacket beingprovided with a-suitable inlet 73 and outlet ,4" for the cooling agentsuch as water. The outlet is from the condenser is provided with apressure valve C and leads to a suitable trap or condensed liquidcollector F having a battle Z and a suitable draw-off pipe m. The trapis provided with an outlet n for non-condensed gases or vapors, saidoutlet leading to a suitable compressor Gr, diagrammatically shown,wherein said vapors or gases are compressed, whence they pass throughthe outlet 6 of the compressor into an expansion chamber H. The effectof expanding the mixture of compressedgases and vapors in chamber Hresults in the reduction of the temperature thereof to such extent thatpractically all the condensable vapors are-liquefied in said chamber andmay be drawn off through pipe 3). The expansion chamber H is providedwith a gas or vapor outlet q through which the residuary, uncondensedvapors or gases pass, whereupon they may be subjected to such furtheruse or treatment as is found desirable.

Referring to Figure 3, A is a still providod with an oil inlet a and aninlet for inert gas 6 The still is heated by means of carbon electrodes0 c", which may be of substantially the same form described inconnection with Figures 1 and 2, the main difference in the method ofheating consisting, however, in spacing the electrodes apart, wherebyarcing is produced within the body of the oil. The electrodes 0 0 areprovided with suitable electrical connections 6 6 respectively. It willbe understood that the still illustrated in Figure '3 may also beprovided with means, similar to that shown in Figures 1 and 2, such astubular electrode f having terminals 9 7: for electrically heating theoil vapors.

. From the foregoing description of the apparatus, its mode of use willbe readilyunderstood by those skilled in the art from the detaileddescription of applicants process. It will be observedthat the pressurevalves C, C in Figures 1 and 2, re spectively, are positioned beyond thecondensing coil, thereby maintaining the vapors and gases under pressureduring the conill ill)

my process may be carried out with different steps and with theassistance of different apparatus from that described, without, however,departing from the scope of my invention, and, accordingly, I intendthat all matter contained in the above description, shall be interpretedas illustrative and not in a limiting sense.

i I realize that considerable variation is possible in the details ofthe process herein shown, and I do not intend to limit myself thereto,except as pointed out in the following claims, in which it is myintention to claim all the novelty inherent in the process as broadly asis permitted by the state of the art.

Any suitable chemical equivalents to the reagents described herein, mayalso be used.

What I claim as new and desire to secure by Letters Patent, is

l. The process of converting kerosene into a low boiling hydrocarbondistillate,

consisting in subjecting the kerosene first in the liquid and then inthe vapor state-t0 contact with carbon heated electrically to atemperature ranging from a bright red to white heat under a regulatedpressure in excess of atmospheric and below five hundred pounds to thesquare inch, and maintaining such pressure. upon the hydrocarbons bothduring their conversion and throughout the course of their cooling andcondensation.

v 2. The process of converting high boiling hydrocarbons into a lowboiling hydrocarbon distillate, consisting in subjecting the liquidhydrocarbons and their evolved vapors, in a confined space, to contactwith carbon heated electrically to a dissociating temperature not abovea white heat, and maintaining a regulated pressure in excess ofatmospheric and below two hundred pounds to the square inch upon thehydrocarbons both during their conversion and subsequent cooling andcondensation.

3. The method of converting kerosene into a low boiling hydrocarbondistillate, which consists in dissociating and distilling the highboiling hydrocarbons by subjecting the hydrocarbons first in the liquidstate and .then in the vapor state to carbon resistance means heatedelectrically to a temperature ranging from between a cherry red and awhite heat under a pressure in excess of atmospheric, cooling all the'vapors passing from the still while under such pressure to condense theheavier fractions thereof, and

simultaneously returning the condensed heavier fractions to the still toundergo therein further treatment, leading off and condensing the lightvapors, and maintaining such distillation pressure on saidvaporsthroughout their course to and while undergoing condensation 4. Aprocess of cracking hydrocarbon oils that consists in maintaining abodyof oil in vaporization,

a combined vaporizing and cracking chamber, applying heat locally to thebody of liquid to vaporize it, and applying heat locally to the vaporsinthe chamber above the liquid level of sufficient intensity to crack saidvapors, and condensing the cracked vapors under superatmosphericpressure, self-imposed by the evolution of vapors in the chamber.

5. A process of cracking hydrocarbon oils that consists in maintaining abody of oil in a combined vaporizing and cracking cham-' ber, applyingheat locally to the body of liquid to vaporize it by a heater immersedtherein, and applying heat locally to the vapors in the chamber abovethe liquid level by a heat generator within the chamber of suflicientintensity to crack said vapors, and condensing the cracked vapors undersuperatmospheric pressure, self-imposed by the evolution of vaporsin'the chamber.

6. A process of cracking hydrocarbon oil which comprises maintaining abody ofliquid oil in a combined vaporizing and cracking chamber, heatingthe body of oil to efi'ect its vaporization, electrically heating theevolved vapors above the body of oil in said chamber to sufficientlyintense heat and under self imposed superatmospheric pressure to crackthe vapors and condensing the cracked vapors.

7 A process of cracking hydrocarbon oil which comprises maintaining abody of oil in a combined vaporizing and cracking chamber, heating saidbody of oil to effect its .applying heat to the vapors in the chamberabove the body of oil of sufiicient intensity to crack the vapors, andmaintaining superatmospheric pressure on the oil under treatment.

8. A process of cracking hydrocarbon oil which comprises maintaining abody of oil in a combined vaporizing and cracking chamber, heating saidbody'of oil to effect its vaporization, applying heat to the vapors inthe chamber above the body of oil of suflicient intensity to crack thevapors maintaining superatmospheric pressure on the oil under treatment,separating out and retlirning for retreatment certain heavier conestituents or the evolved vapors, and condensing the vapors of. desiredvolatility.

9. The process of converting heavy hydrocarbon oils into low boilinghydrocarbon distillates consisting in subjecting a relatively stationarybody of such heavy hydro carbon oils to direct contact with an electriscally heated noninetallic resistor immersed in the body of oil, whilethe'body of oil is kept under pressure, and passing the evolved vaporsinto contact with a second electrically heated non-metallic resistorwhich serves to convert anyunconverted. vapors carried by the convertedvapors.

10. The process of converting liquid low boiling hydrocarbon distillate,which consists in subjecting both the liquid hydrocarbon and its evolvedvapors, While the liquid hydrocarbon is in a quiescent state, to a localdecomposing heat ranging in tentperature between 800 C. and 2000 6.,While subjecting both the liquid hydrocarbon and its evolved vapors to acontrolled pressure in excess of 5 atmospheres and collecting andcondensing the resulting cracked vapors 11. The process of convertingliquid hydrocarbons boiling abo e 200 G. into a low boiling hydrocarbondistillate, consist- 1 ing in subjecting the liquid hydrocarbon,

:neiaace While in a quiescent state, to contact with a n0n-1netallicresistor heated to between a red and a White heat by the passage of anelectric current, and maintaining in contact with the evolved vapors anon-metallic resistor heated to between a red and a White heat by thepassage of an electric current,

and subjecting both the liquid hydrocarbons and the hydrocarbon vaporsto a controlled pressure, principally autogenous, in excess of liveatmospheres, and collecting and condensing the resulting cracked vapors.

In testimony whereof l have signed my name to this specification.

@TTU P, AMEND

